US5894062A - Process for the recovery of polyhydroxyalkanoic acid - Google Patents

Process for the recovery of polyhydroxyalkanoic acid Download PDF

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US5894062A
US5894062A US08/793,832 US79383297A US5894062A US 5894062 A US5894062 A US 5894062A US 79383297 A US79383297 A US 79383297A US 5894062 A US5894062 A US 5894062A
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pha
solution
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temperature
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US08/793,832
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John Macdonald Liddell
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CJ CheilJedang Corp
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Monsanto Co
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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/62—Carboxylic acid esters
    • C12P7/625—Polyesters of hydroxy carboxylic acids
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
    • C08G63/88—Post-polymerisation treatment
    • C08G63/89—Recovery of the polymer
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S435/00—Chemistry: molecular biology and microbiology
    • Y10S435/8215—Microorganisms
    • Y10S435/822—Microorganisms using bacteria or actinomycetales
    • Y10S435/829—Alcaligenes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S435/00—Chemistry: molecular biology and microbiology
    • Y10S435/8215—Microorganisms
    • Y10S435/822—Microorganisms using bacteria or actinomycetales
    • Y10S435/874—Pseudomonas

Definitions

  • THIS INVENTION relates to a process for the recovery of polyhydroxyalkanoic acid.
  • the invention therefore comprises a process in which a polymer of a hydroxyalkanoic acid (PHA)is recovered from matter derived from living organisms which comprises dissolving the PHA in a solvent which is a lower ketone, dialkyl ether, a lower alcohol or an ester thereof, separating the solution from such matter and recovering PHA from the solution.
  • a solvent which is a lower ketone, dialkyl ether, a lower alcohol or an ester thereof
  • the process is very suitable for the recovery of polymers and copolymers of hydroxybutyric acid for example a polymer of hydroxybutyric and hydroxyvaleric acids.
  • the PHA be precipitated from the solution by adding water.
  • Solvents which are immiscible with water may also be used in which case the PHA may be recovered by evaporating the solvent or by temperature cycling by which the PHA is dissolved at a high temperature and the solution cooled to precipitate PHA.
  • the solvent may in the latter case be reused for further extraction of PHA but it is desirable if this is done to replace at least part of the solvent by fresh solvent so as to prevent undue build up of impurities on continued recycle of the solvent.
  • Fresh solvent may be produced by distilling pure solvent from used impure solvent.
  • Preferred water miscible solvents include lower ketones, especially acetone and lower alcohols for example methanol, ethanol, or a propanol which is suitably isopropanol.
  • Such solvents may be used in the presence or absence of water.
  • ethanol/water mixtures may be used which can be but are not limited to azeotropic compositions.
  • the vegetable matter contains oil it is preferred that the oil be extracted from the vegetable matter before it is treated according to this invention. This may be done by pressing the vegetable matter to expel oil and/or by extracting it with a water immiscible solvent which is suitably a paraffin or cyclo-paraffin containing for example 4 to and preferably 5 to 8 carbon atoms.
  • the water immiscible solvent is preferably one which does not dissolve substantial quantities of PHA.
  • oil and PHA may be extracted together from vegetable matter by dissolving them in a solvent, separating the solids from undissolved vegetable matter and separating the PHA from the solution, for example by cooling to precipitate it or adding a liquid which reduces its solubility in the solvent, for example water.
  • the solvent extraction is preferably carried out at a temperature above 100° C. and preferably above 120° C. It is however preferred that the temperature should not substantially exceed 150° C. in order to avoid depolymerisation of the PHA.
  • a ratio of 1.5:1 to 10:1 of solvent (ml) to solid (grams) should be used so as to secure easy handling of the mixture of vegetable matter and solvent and effective recovery of PHA.
  • PHA may be recovered by cooling the solution for example to 20-80° C. and preferably 30 to 50°, or by evaporating the solvent. If a water miscible solvent is employed the solution may be cooled to below 100° C.
  • the higher alcohols for example C 4 to C 10 alcohols, for example butanol, and amyl alcohol esters containing C 4 to C 10 carbon atoms for example ethyl acetate and amyl acetate and higher ketones for example cyclo hexanone, and methyl isobutyl ketone.
  • PHA precipitated by the addition of water may be in the form of a gel. This may be compressed to expel solvent and/or water to leave flakes of PHA.
  • the vegetable matter should contain substantial quantities of PHA for example 10 to 60% by weight of PHA.
  • Spent rape seed meal (the residue left after conventional extraction methods for rape seed oil including cooking, crushing and hexane extraction)was mixed with poly 3-hydroxybutyrate polymer particles in a ratio of 2:1 weight of rape meal to polymer.
  • the polymer solution was cooled to 70° C. with agitation of the solution at which point the polymer formed a rigid opaque gel in the solvent.
  • the polymer was recovered from the solvent phase by compressing the polymer gel between closely spaced rotating rollers producing flakes of polymer largely free of solvent.
  • the expressed solvent could be reused in further extractions directly or after appropriate purification methods, i.e. evaporation.
  • the resulting polymer flakes were further freed by solvent by heating to 80° C.
  • the resulting polymer flakes were solvent free and comprised polymer which was 99.7% pure and of molecular weight 650,000.
  • Transgenic Arabidopsis thaliana containing 15% polyhydroxybutyric acid as described by Poirier et al. Bio/Technology (1995) 13 142-150 may be treated as follows:

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Zoology (AREA)
  • Wood Science & Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Chemical & Material Sciences (AREA)
  • Microbiology (AREA)
  • Polymers & Plastics (AREA)
  • Biochemistry (AREA)
  • Biotechnology (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Medicinal Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Polyesters Or Polycarbonates (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Heterocyclic Compounds That Contain Two Or More Ring Oxygen Atoms (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

A hydroxyalkanoic acid (PHA)is recovered from matter derived from living organisms by dissolving the PHA in a solvent which is a lower ketone, dialkyl ether or a lower alcohol or a monocarboxylic acid ester thereof, separating the solution from such matter and recovering PHA from the solution.

Description

THIS INVENTION relates to a process for the recovery of polyhydroxyalkanoic acid.
It has been found that it is possible to produce polyhydroxyalkanoic acid for example polyhydroxybutyric acid in microorganisms, for example Alcaligenes and in plants. The recovery of the polymer, especially from plants in a state of sufficient purity for it to be useable as a plastics material presents difficulties however. Matter derived from plants for example seeds and fruits is herein referred to as vegetable matter.
Surprisingly we have found that it is possible to carry out an effective separation of polyhydroxy-alkanoic acid from matter derived from organisms which contains it by dissolving the polyhydroxyalkanoic acid (PHA) in a solvent which is a lower ketone, dialkyl ether or a lower alcohol or an ester thereof, separating the solution so formed from undissolved matter and recovering PHA from the solution.
The invention therefore comprises a process in which a polymer of a hydroxyalkanoic acid (PHA)is recovered from matter derived from living organisms which comprises dissolving the PHA in a solvent which is a lower ketone, dialkyl ether, a lower alcohol or an ester thereof, separating the solution from such matter and recovering PHA from the solution.
The process is very suitable for the recovery of polymers and copolymers of hydroxybutyric acid for example a polymer of hydroxybutyric and hydroxyvaleric acids.
It is often desirable to crush or mill the vegetable matter prior to contacting it with the solvent in order to permit more intimate contact of the solution with the PHA.
If the solvent is miscible with water it is preferred that the PHA be precipitated from the solution by adding water. Solvents which are immiscible with water may also be used in which case the PHA may be recovered by evaporating the solvent or by temperature cycling by which the PHA is dissolved at a high temperature and the solution cooled to precipitate PHA. The solvent may in the latter case be reused for further extraction of PHA but it is desirable if this is done to replace at least part of the solvent by fresh solvent so as to prevent undue build up of impurities on continued recycle of the solvent. Fresh solvent may be produced by distilling pure solvent from used impure solvent.
Preferred water miscible solvents include lower ketones, especially acetone and lower alcohols for example methanol, ethanol, or a propanol which is suitably isopropanol. Such solvents may be used in the presence or absence of water. For example ethanol/water mixtures may be used which can be but are not limited to azeotropic compositions.
If the vegetable matter contains oil it is preferred that the oil be extracted from the vegetable matter before it is treated according to this invention. This may be done by pressing the vegetable matter to expel oil and/or by extracting it with a water immiscible solvent which is suitably a paraffin or cyclo-paraffin containing for example 4 to and preferably 5 to 8 carbon atoms. The water immiscible solvent is preferably one which does not dissolve substantial quantities of PHA.
If desired oil and PHA may be extracted together from vegetable matter by dissolving them in a solvent, separating the solids from undissolved vegetable matter and separating the PHA from the solution, for example by cooling to precipitate it or adding a liquid which reduces its solubility in the solvent, for example water.
The solvent extraction is preferably carried out at a temperature above 100° C. and preferably above 120° C. It is however preferred that the temperature should not substantially exceed 150° C. in order to avoid depolymerisation of the PHA. Suitably a ratio of 1.5:1 to 10:1 of solvent (ml) to solid (grams) should be used so as to secure easy handling of the mixture of vegetable matter and solvent and effective recovery of PHA. PHA may be recovered by cooling the solution for example to 20-80° C. and preferably 30 to 50°, or by evaporating the solvent. If a water miscible solvent is employed the solution may be cooled to below 100° C. for example to a temperature in the range 40 to 90 and water added for example 10 to 50% and preferably 25 to 35% by volume to the solution to cause precipitation. In general the higher the molecular weight of the monomer units in the PHA the lower the temperatures necessary to carry out the solution step. Among solvents of low water miscibility which may be used are included the higher alcohols for example C4 to C10 alcohols, for example butanol, and amyl alcohol esters containing C4 to C10 carbon atoms for example ethyl acetate and amyl acetate and higher ketones for example cyclo hexanone, and methyl isobutyl ketone.
Based on the Hildebrand expression for the square root of the cohesive energy density (`The Solubility of Non Electrolytes`, Hildebrand, J. H., Scott, R. L. (1950)), the solubility parameter, it is found that in general solvents having solubility parameters between 15 and 30 J1/2 /cm3/2 are preferred for a PHA such as poly 3-hydroxybutyrate or poly 3-hydroxy-butyrate/poly 3-hydroxyvalerate copolymers.
PHA precipitated by the addition of water may be in the form of a gel. This may be compressed to expel solvent and/or water to leave flakes of PHA.
It is preferred that the vegetable matter should contain substantial quantities of PHA for example 10 to 60% by weight of PHA.
It is preferred that vegetable matter after treatment according to this invention be used as animal feed. It is preferred therefore that the solvents used in this invention should be acceptable in animal feed so that residues of the solvents may be tolerated in it. It is however preferred that substantially all of the solvent be removed from the vegetable residue
EXAMPLE 1
Spent rape seed meal (the residue left after conventional extraction methods for rape seed oil including cooking, crushing and hexane extraction)was mixed with poly 3-hydroxybutyrate polymer particles in a ratio of 2:1 weight of rape meal to polymer.
20 g of the mixture was suspended by agitation in 100 ml of hexanol solvent and heated to 140° C. The solution was maintained at 140° for 30 minutes then the rape meal solids filtered off by pressure filtration at 2 bar using a metal mesh filter cloth.
The polymer solution was cooled to 70° C. with agitation of the solution at which point the polymer formed a rigid opaque gel in the solvent. The polymer was recovered from the solvent phase by compressing the polymer gel between closely spaced rotating rollers producing flakes of polymer largely free of solvent. The expressed solvent could be reused in further extractions directly or after appropriate purification methods, i.e. evaporation.
The resulting polymer flakes were further freed by solvent by heating to 80° C. The resulting polymer flakes were solvent free and comprised polymer which was 99.7% pure and of molecular weight 650,000.
EXAMPLE 2
Transgenic Arabidopsis thaliana containing 15% polyhydroxybutyric acid as described by Poirier et al. Bio/Technology (1995) 13 142-150 may be treated as follows:
Suspend by agitation 20 g of the dried material in 100 ml of isopropanol and heat in a pressurised vessel to 140° C. for 30 minutes to dissolve the poly 3-hydroxy-butyric acid. After polymer dissolution remove the solids from the liquid by filtration of the solution. (Maintain the filtered solution of poly 3-hydroxybutyrate in isopropanol under pressure to prevent evaporation of the solvent). Recover polymer from the solvent by adding at least 30 ml of water or by reducing the solution temperature to 30 to 60° C. and separate the solid poly-hydroxybutyric acid by filtering or centrifuging.

Claims (12)

I claim:
1. A process in which a polymer or copolymer of hydroxyalkanoic acid (PHA) is recovered from matter derived from living organisms by dissolving the PHA at a temperature above 100° C. in a solvent which is a lower ketone, dialkyl ether or a lower monoalcohol or a monocarboxylic acid ester thereof, separating the solution from such matter and recovering PHA from the solution.
2. A process as claimed in claim 1 in which the solvent is a lower ketone, dialkyl ether or a lower alcohol.
3. A process as claimed in claim 2 in which the solvent has 1 to 10 carbon atoms.
4. A process as claimed in claim 1 in which the solvent is an ester having from 1 to 12 carbon atoms.
5. A process as claimed in claim 1 in which the matter derived from living organisms is derived from microorganisms or plants.
6. A process as claimed in claim 5 in which the matter is derived from oil bearing plant matter by extracting the oil and crushing and/or milling it.
7. A process as claimed in claim 6 in which the oil extraction is accomplished at least in part by dissolving the oil in a water immiscible solvent in which the PHA is substantially insoluble.
8. A process as claimed in claim 1 in which the PHA is a polymer or copolymer of hydroxybutyric acid.
9. A process as claimed in claim 1 in which PHA is dissolved at a temperature in the range 100 to 150° C. and is recovered by cooling the solution to a temperature in the range 20 to 80° C. or, if the solvent is water miscible, cooling to a temperature of at most 100° C. and adding water.
10. A process as claimed in claim 1, 5, or 6 in which plant matter remaining after the extraction of PHA and reduction of its solvent content is fed to animals.
11. A process as claimed in claim 4, wherein the ester has from 4 to 10 carbon atoms.
12. A process as claimed in claim 9, wherein the solution is cooled to a temperature from 30 to 50° C., or if the solvent is water miscible, to a temperature of 20 to 90° C.
US08/793,832 1994-08-18 1995-08-15 Process for the recovery of polyhydroxyalkanoic acid Expired - Lifetime US5894062A (en)

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GB9416690 1994-08-18
GB9416690A GB9416690D0 (en) 1994-08-18 1994-08-18 Process for the recovery of polyhydroxyalkanoic acid
PCT/GB1995/001926 WO1996006179A1 (en) 1994-08-18 1995-08-15 Process for the recovery of polyhydroxyalkanoic acid

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EP (1) EP0776372B1 (en)
JP (1) JP3580824B2 (en)
AT (1) ATE192194T1 (en)
AU (1) AU3188395A (en)
CA (1) CA2197783C (en)
DE (1) DE69516523T2 (en)
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Cited By (31)

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Publication number Priority date Publication date Assignee Title
WO2001068890A2 (en) * 2000-03-10 2001-09-20 Metabolix, Inc. Method of extracting polyhydroxyalkanoate from a solution
US20030158274A1 (en) * 2001-12-18 2003-08-21 Luhua Zhong Methods of making intermediates from polyhydroxyalkanoates
WO2004076582A1 (en) 2003-02-21 2004-09-10 Metabolix Inc. Pha blends
US20040220355A1 (en) * 2003-02-21 2004-11-04 Whitehouse Robert S. PHA blends
WO2005049691A1 (en) 2003-11-21 2005-06-02 Kaneka Corporation Process for producing polyhydroxyalkanoate crystal
US20050191629A1 (en) * 2002-08-06 2005-09-01 Walsem Johan V. Polymer extraction methods
US20050222373A1 (en) * 2003-11-21 2005-10-06 Koichi Kinoshita Method for producing polyhydroxyalkanoate crystal
US20050228168A1 (en) * 2003-11-21 2005-10-13 Koichi Kinoshita Method for producing polyhydroxyalkanoate crystal
US20050287654A1 (en) * 2004-06-29 2005-12-29 Karunakaran Narasimhan Process for the solvent-based extraction of polyhydroxyalkanoates from biomass
US20050287653A1 (en) * 2004-06-29 2005-12-29 The Procter & Gamble Company Solvent extraction of polyhydroxyalkanoates from biomass
US20060058501A1 (en) * 2004-09-13 2006-03-16 Walsem Johan V Single solvent polymer extraction methods
US20060057692A1 (en) * 2004-09-15 2006-03-16 Karunakaran Narasimhan Process for the extraction of polyhydroxyalkanoates from biomass
US20060105440A1 (en) * 2004-09-30 2006-05-18 Koichi Kinoshita Method of producing polyhydroxyalkanoate
US20080118963A1 (en) * 2002-09-30 2008-05-22 Noriko Ogawa Method Of Coagulating Poly-3-Hydroxyalkanoic Acid
US20080220505A1 (en) * 2007-03-09 2008-09-11 Jian Yu Recovery and purification of polyhydroxyalkanoates
US20080241886A1 (en) * 2003-10-15 2008-10-02 Hedrrema-Kimmel,Llc Process For the Treatment of Methane Emissions
US7745197B1 (en) 2003-10-15 2010-06-29 Newlight Technologies, Llc Process for the utilization of ruminant animal methane emissions
US8263373B2 (en) 2003-10-15 2012-09-11 Newlight Technologies, Llc Method for producing polyhydroxyalkanoic acid
US8735113B2 (en) 2003-10-15 2014-05-27 Newlight Technologies, Llc Methods and systems for production of polyhydroxyalkanoate
US9040267B2 (en) 2011-03-08 2015-05-26 Newlight Technologies, Llc Polyhydroxyalkanoate production method
US9085784B1 (en) 2012-03-29 2015-07-21 Newlight Technologies, Llc Polyhydroxyalkanoate production methods and materials and microorganisms used in same
US10030135B2 (en) 2012-08-17 2018-07-24 Cj Cheiljedang Corporation Biobased rubber modifiers for polymer blends
US10611903B2 (en) 2014-03-27 2020-04-07 Cj Cheiljedang Corporation Highly filled polymer systems
US10669417B2 (en) 2013-05-30 2020-06-02 Cj Cheiljedang Corporation Recyclate blends
US10786064B2 (en) 2010-02-11 2020-09-29 Cj Cheiljedang Corporation Process for producing a monomer component from a genetically modified polyhydroxyalkanoate biomass
US11078328B1 (en) 2020-10-30 2021-08-03 Robert Whitehouse Sequestered amorphous polyhydroxyalkanoate polymer (SAPP) material derived from cellular biomass and production thereof
US11104761B1 (en) 2020-10-30 2021-08-31 Robert Whitehouse Sequestered amorphous polyhydroxyalkanoate polymer (SAPP) material derived from cellular biomass and production thereof
US11440823B2 (en) 2016-06-23 2022-09-13 Kaneka Corporation Method for producing polyhydroxyalkanoic acid
US11732280B2 (en) 2012-03-29 2023-08-22 Newlight Technologies, Inc. Polyhydroxyalkanoate production methods and materials and microorganisms used in same
US12037628B2 (en) 2009-08-27 2024-07-16 Newlight Technologies, Inc. Polyhydroxyalkanoate production and related processes
US12060597B2 (en) 2011-12-02 2024-08-13 Newlight Technologies, Inc. Polyhydroxyalkanoate production methods and systems for same

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US5942597A (en) * 1995-08-21 1999-08-24 The Procter & Gamble Company Solvent extraction of polyhydroxyalkanoates from biomass
AU751673B2 (en) * 1995-10-26 2002-08-22 Metabolix, Inc. Methods for isolating polyhydroxyalkanoates from plants
US6083729A (en) * 1995-10-26 2000-07-04 Metabolix, Inc. Methods for isolating polyhydroxyalkanoates from plants
US5821299A (en) * 1996-02-16 1998-10-13 The Proctor & Gamble Company Solvent extraction of polyhydroxy-alkanoates from biomass facilitated by the use of marginal nonsolvent
US6087471A (en) * 1997-04-15 2000-07-11 Monsanto Company High temperature PHA extraction using PHA-poor solvents
EP0975788A1 (en) * 1997-04-15 2000-02-02 Monsanto Company Methods of pha extraction and recovery using non-halogenated solvents
ATE458822T1 (en) 1998-04-08 2010-03-15 Metabolix Inc METHOD FOR THE SEPARATION AND PURIFICATION OF BIOPOLYMERS
CA2333005A1 (en) 1998-06-09 1999-12-16 Tillman U. Gerngross Methods and apparatus for the production of amorphous polymer suspensions
JPWO2005049692A1 (en) * 2003-11-21 2007-06-07 株式会社カネカ Process for producing polyhydroxyalkanoate crystals
WO2006035889A1 (en) * 2004-09-30 2006-04-06 Kaneka Corporation Process for producing polyhydroxyalkanoate
WO2010067543A1 (en) 2008-12-09 2010-06-17 株式会社カネカ Method for producing poly-3-hydroxyalkanoate and agglomerate of poly-3-hydroxyalkanoate
US20110300592A1 (en) 2008-12-09 2011-12-08 Kaneka Corporation Method for producing poly-3-hydroxyalkanoic acid
AU2014217519B2 (en) * 2013-02-14 2016-04-28 Veolia Water Solutions & Technologies Support Process for the extraction of polyhydroxyalkanoates from biomass

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